Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
  • C07C209/24—Preparation of compounds containing amino groups bound to a carbon skeleton by reductive alkylation of ammonia, amines or compounds having groups reducible to amino groups, with carbonyl compounds
  • C07C209/26—Preparation of compounds containing amino groups bound to a carbon skeleton by reductive alkylation of ammonia, amines or compounds having groups reducible to amino groups, with carbonyl compounds by reduction with hydrogen
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D295/00—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms
  • C07D295/02—Heterocyclic compounds containing polymethylene-imine rings with at least five ring members, 3-azabicyclo [3.2.2] nonane, piperazine, morpholine or thiomorpholine rings, having only hydrogen atoms directly attached to the ring carbon atoms containing only hydrogen and carbon atoms in addition to the ring hetero elements
  • C07D295/023—Preparation; Separation; Stabilisation; Use of additives
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2601/00—Systems containing only non-condensed rings
  • C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
  • C07C2601/14—The ring being saturated

Definitions

• the present invention relates to a process for preparing an amine by reacting an aldehyde and/or ketone with hydrogen and a nitrogen compound selected from the group of primary and secondary amines in the presence of a heterogeneous catalyst.
• the process products find use, inter alia, as intermediates in the preparation of fuel additives (U.S. Pat. No. 3,275,554; DE-A-21 25 039 and DE-A-36 11 230), surfactants, medicaments and crop protectants, hardeners for epoxy resins, catalysts for polyurethanes, intermediates for preparing quaternary ammonium compounds, plasticizers, corrosion inhibitors, synthetic resins, ion exchangers, textile assistants, dyes, vulcanization accelerants and/or emulsifiers.
• DE-A-211 82 83 (BASF AG) relates to a process for preparing secondary or tertiary aliphatic or cycloaliphatic amines using a Pd/Ag catalyst which is not a coated catalyst.
• the support material is in particular SiO 2 .
• EP-A1-7093 (BASF AG) relates to the preparation of N-aralkyl-2,6-dimethylmorpholines, for example fenpropimorph, over Pd/Ag catalysts which are not coated catalysts.
• the support material is in particular SiO 2 .
• a particularly preferred support is ZrO 2 .
• German patent application No. 102005019540.7 of Apr. 27, 2005 (BASF AG) relates to a process for preparing an amine by reacting an aldehyde and/or ketone with hydrogen and a nitrogen compound selected from the group of primary and secondary amines, in the presence of a heterogeneous catalyst, the catalyst being a catalyst packing which can be prepared by applying at least one catalytically active metal and/or at least one compound of this metal to a fabric, a knit or a foil as a support material.
• DMCHA N,N-dimethylcyclohexylamine
• EP-A1-611 137 (Sumitomo Chem. Comp.) relates to the reductive amination of cyclic ketones, a corresponding imino compound being prepared in a first stage and then hydrogenated.
• EP-A2-312 253 (Kao Corp.) describes the use of specific copper catalysts in the preparation of N-substituted amines from alcohols or aldehydes.
• the process should include a catalyst of high activity, which exhibits particularly high selectivity in the reaction.
• a process for preparing an amine by reacting an aldehyde and/or ketone with hydrogen and a nitrogen compound selected from the group of primary and secondary amines in the presence of a heterogeneous catalyst, wherein the catalyst is a coated catalyst which comprises at least one metal of group VIII of the Periodic Table of the Elements as a hydrogenating metal and additionally a promoter on an oxidic support, at least 80% of the metal of group VIII of the Periodic Table of the Elements being present in a layer between the surface of the catalyst and a penetration depth which is not more than 80% of the radius of the catalyst, calculated from the surface of the catalyst.
• the metal of group VIII of the Periodic Table of the Elements is preferably present essentially in homogeneous distribution in the defined shell.
• the promoter is preferably present in essentially homogeneous distribution over the entire cross section of the catalyst.
• the advantages of the process according to the invention include good chemical activity of the catalyst, the high mechanical stability of the catalyst support and the very good selectivity of the catalyst.
• the overhydrogenation of the starting material (ketone or aldehyde) to the corresponding alcohol is observed only to a very small degree.
• feedstock cost advantages consequently arise.
• the process according to the invention can also produce active ingredients with defined stereochemistry in a particularly advantageous manner, since the stereochemical information is preserved in the course of the synthesis with high selectivity. Side reactions, such as the unselective transfer of substituents, are also observed only to a slight degree, if at all, in the synthesis of unsymmetrically substituted amines.
• the high activity of the catalyst used in accordance with the invention further enables the performance of the reaction at reduced pressure and/or reduced temperature, which additionally increases the selectivity of the reaction.
• the possibility of being able to perform the reductive amination at lower pressure, for example 90 bar instead of 140 bar, with nevertheless very high space-time yields enables the commissioning of production plants with significantly lower capital costs (lower pressure level).
• the catalyst used in the process according to the invention is characterized as follows and can be prepared as follows. The preparation is also described in the prior BASF patent application PCT/EP2005/011026 of Oct. 13, 2005.
• At least 80% of the metal of group VIII of the Periodic Table of the Elements is present in a layer between the surface of the catalyst and a penetration depth which is not more than 80% of the radius of the catalyst, calculated from the surface of the catalyst.
• the catalyst used has a diameter of from 1.5 to 10 mm, at least 80% of the metal of group VIII of the Periodic Table of the Elements being present in a layer between the surface of the catalyst and a penetration depth of not more than 1000 ⁇ m, calculated from the surface of the catalyst.
• the metal of group VIII of the Periodic Table of the Elements is preferably present in essentially homogeneous distribution in the defined shell.
• the promoter is preferably present in essentially homogeneous distribution over the entire cross section of the catalyst.
• the invention thus provides a catalyst in which the metal of group VIII of the Periodic Table of the Elements forms a coating structure in the catalyst.
• the catalyst used in accordance with the invention preferably has a diameter in the range from 1.5 to 9 mm.
• the diameter of the catalysts used in accordance with the invention is from 2.0 to 5 mm, in particular from 2.5 to 3.5 mm.
• the metal of group VIII of the Periodic Table of the Elements is present in a layer between the surface of the catalyst and a penetration depth of not more than 1000 ⁇ m, calculated from the surface of the catalyst.
• the catalyst used in accordance with the invention comprises a metal of group VIII of the Periodic Table of the Elements (Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt). In a preferred embodiment of the present invention, it is palladium.
• the catalyst used in accordance with the invention additionally comprises at least one promoter.
• it may comprise further metals of group VIII, IB and IIB of the Periodic Table of the Elements (Cu, Ag, Au, Zn, Cd, Hg).
• the catalysts used in accordance with the invention comprise, in addition to the metal of group VIII of the Periodic Table of the Elements, also at least one metal from group IB of the Periodic Table of the Elements. Particular preference is given here to silver.
• the catalyst used in accordance with the invention comprises palladium and silver.
• the catalyst used in accordance with the invention may have any shapes, for example extrudates, hollow extrudates, tablets, rings, spherical particles or spheres. It is preferred when the catalyst is in the form of an extrudate.
• the metals may be present in pure metallic form, but also in the form of compounds, for example in the form of metal oxides. Under the operating conditions of the amination process, they are generally present in the form of metals.
• the conversion of any oxides to metals can be effected in the manner known to those skilled in the art before the catalyst is used in a hydrogenation process within or outside a hydrogenation reactor, for example by prereduction and, if required or advantageous for manipulations with the prereduced catalyst, subsequent surface passivation.
• the content in the catalyst of metal or metals of group VIII of the Periodic Table, especially palladium is preferably at least 0.01% by weight, more preferably at least 0.1% by weight, in particular at least 0.15% by weight. This content is preferably at most 5% by weight, more preferably at most 1% by weight, in particular at most 0.6% by weight. Although lower and higher contents are possible, they are normally economically unsatisfactory owing to excessively low activity or excessively high raw material costs. In a particularly preferred embodiment, only one hydrogenating metal, especially palladium, is used.
• the ratio of the amounts of hydrogenation metal of group VIII of the Periodic Table of the Elements and additives or dopants is a parameter to be optimized in the individual case.
• the atomic ratio of metal of group VIII of the Periodic Table of the Elements, more preferably palladium, to the promoter, more preferably silver, is preferably 0.1-10, more preferably 2-7, in particular 2.5-6.
• the oxidic support of the catalyst used in accordance with the invention is preferably alumina, more preferably in a mixture of ⁇ -, ⁇ - and ⁇ -alumina.
• the support may also comprise other additives to a certain extent.
• other inorganic oxides such as oxides of metals of group IA, IIIB, IVB, IIIA and IVA of the Periodic Table of the Elements may be present, especially silicon dioxide, titanium dioxide, zirconium dioxide, zinc oxide, magnesium oxide, sodium oxide and/or calcium oxide.
• the maximum content in the support of such oxides other than alumina is dependent upon the oxide actually present, but can be determined in the individual case with reference to the X-ray diffractogram of the hydrogenation catalyst, since a change in the structure is accompanied by a significant change in the X-ray diffractogram.
• the content of such oxides other than alumina is below 50% by weight, preferably below 30% by weight, more preferably below 10% by weight.
• the purity of the alumina is preferably higher than 99%.
• a suitable aluminum-containing raw material preferably boehmite
• a peptizing agent such as water, dilute acid or dilute base.
• the acid used is, for example, a mineral acid, for instance nitric acid, or an organic acid, for instance formic acid.
• the base used is preferably an inorganic base, for instance ammonia.
• the acid or base is generally dissolved in water.
• the peptizing agent used is preferably water or dilute aqueous nitric acid.
• the concentration of the nonaqueous fraction in the peptizing agent is generally 0-10% by weight, preferably 0-7% by weight, more preferably 0-5% by weight.
• Boehmite ( ⁇ -AlO(OH)) is a widespread commercial product, but can also be prepared in a known manner immediately before the actual support preparation by precipitation from a solution of an aluminum salt, for example aluminum nitrate, with a base, removal, washing, drying and calcining of the precipitated solid.
• boehmite is used in the form of a powder.
• a suitable commercial boehmite powder is, for example, Versal® 250, which is available from UOP.
• the boehmite is treated with the peptizing agent by moistening it with the peptizing agent and mixing it intensively, for example in a kneader, mixer or edge-runner mill. The peptization is continued until the material is readily shapeable.
• the material is shaped to the desired shaped support bodies by customary methods, for example by strand pressing, extrusion, tableting or agglomeration. Any known method is suitable for the shaping. If required or advantageous, customary additives may be used. Examples of such additives are extruding or tableting assistants such as polyglycols or graphite.
• additives which, in a known manner, influence the pore structure of the support after calcination as burnout substances to the support raw material before the shaping, for example polymers, fibrous substances, natural burnout substances such as nutshell meals, or other customary additives.
• the measures necessary for this purpose are known per se to those skilled in the art.
• the shaped bodies are dried in a customary manner generally at a temperature above 60° C., preferably above 80° C., more preferably above 100° C., especially at a temperature in the range of 120-300° C.
• the drying is continued until water present in shaped bodies has escaped essentially fully from the shaped bodies, which is generally the case after a few hours.
• Typical drying times are in the range from 1 to 30 hours and are dependent upon the drying temperature set, a higher temperature shortening the drying time.
• the drying can be accelerated further by employing a reduced pressure.
• the shaped bodies are converted to the finished support by calcination.
• the calcination temperature is generally in the range of 900-1150° C., preferably in the range of 1000-1120° C., more preferably in the range of 1050-1100° C.
• the calcination time is generally between 0.5 and 5 hours, preferably between 1 and 4 hours, more preferably between 1.5 and 3 hours.
• the calcination is effected in a customary oven, for example in a rotary oven, in a tunnel oven, in a belt calciner or in a chamber oven. The calcination can directly follow the drying without intermediate cooling of the shaped bodies.
• the catalysts usable in accordance with the invention and obtained in this way have a specific surface area (BET, Brunauer-Emmet-Teller, determined to DIN 66131 by nitrogen adsorption at 77 K) of 20-250 m 2 /g, preferably 50-150 m 2 /g, in particular 60-90 m 2 /g.
• the surface area can be varied by known methods, especially use of finely divided or coarse starting materials, calcination time and calcination temperature.
• the pore volume can also be varied in a known manner, it is generally, determined by means of mercury porosimetry, in a range of 0.3-1.0 ml/g, preferably in a range of 0.4-0.9 ml/g, more preferably 0.5-0.8 ml/g.
• the active composition and, if appropriate, further additives are deposited on the support thus produced.
• This X-ray diffractogram is determined as described in EP 0 992 284 A2 on page 9 lines 6 to 9.
• X-ray diffractograms are characteristic of the specific structure of the material analyzed.
• the structure of the inventive catalyst is defined adequately by occurrence of the abovementioned reflections.
• any further reflections may also occur in the X-ray diffractogram of the catalyst used in accordance with the invention.
• the active composition and, if appropriate, further additives may be deposited onto the support thus obtained for the catalyst used in accordance with the invention.
• the preferred method is impregnation with a solution of the substances and/or compounds to be deposited, which are converted to the substances to be deposited in the course of the further catalyst preparation.
• the substances to be deposited may be deposited individually and/or in portions in a plurality of process steps, or together and fully in one process step. Preference is given to combined deposition in one impregnation step.
• the supported catalyst is dried and converted by calcining and, if appropriate, other known aftertreatment methods, for example activation and subsequent surface passivation, to the ready-to-use catalyst.
• Impregnation processes for depositing active components, additives and/or dopants on a support are known.
• the support is impregnated with a solution of salts of the components to be deposited, the volume of the solution being such that the solution is absorbed virtually fully by the pore volume of the support (“incipient wetness” method).
• concentration of the salts in the solution is such that, after impregnation and conversion of the supported catalyst to the finished catalyst, the components to be deposited are present on the catalyst in the desired concentration.
• the salts are selected such that they do not leave behind any residues which are troublesome in the catalyst preparation or its later use. Usually, nitrates or ammonium salts are used.
• the catalyst used in accordance with the invention is prepared preferably by one-stage impregnation of the support by the incipient wetness method with a nitric acid solution of the nitrates of the metals to be deposited.
• an impregnation solution which comprises palladium nitrate and palladium nitrite together is used.
• the impregnation solution is preferably also the metal of group IB of the Periodic Table of the Elements, preferably silver nitrate.
• the pH of the impregnation solution is at most 5, preferably at most 2, more preferably at most 1, in particular at most 0.5.
• the lower limit of the pH is generally 0.2, preferably 0.3, more preferably 0.5.
• a preferred pH range is, for example, from 0.2 to 2, in particular from 0.3 to 0.5.
• the impregnated support is typically dried, generally at a temperature above 60° C., preferably above 80° C., more preferably above 100° C., in particular at a temperature in the range of 120-300° C.
• the drying is continued until water present in the impregnated catalyst has escaped essentially fully, which is generally the case after a few hours.
• Typical drying times are in the range of 1-30 hours and are dependent upon the drying temperature set, a higher drying temperature shortening the drying time.
• the drying can be accelerated further by employing a reduced pressure.
• the impregnated catalyst is dried with simultaneous movement of the impregnated support material, for example in a rotary tube oven.
• the air stream used for drying is conducted in countercurrent through the rotary tube.
• the catalyst is prepared in a customary manner by calcining.
• This calcination serves essentially to convert the impregnated salts to the components to be deposited or precursors of such components, and differs in this respect from the calcination described above, which serves for the preparation of the support material and of the support structure.
• this calcination essentially decomposes the nitrates to metals and/or metal oxides, which remain in the catalyst, and to nitrous gases, which escape.
• the calcination temperature is generally 200-900° C., preferably 280-800° C., more preferably 300-700° C.
• the calcination time is generally between 0.5 and 20 hours, preferably between 0.5 and 10 hours, more preferably between 0.5 and 5 hours.
• the calcination is effected in a customary oven, for example in a rotary tube oven, in a belt calciner or in a chamber oven. The calcination can follow the drying directly without intermediate cooling of the supported and dried catalyst.
• the drying and the calcination of the catalyst are combined in a rotary tube oven.
• the catalyst After the calcination, the catalyst is in principle ready for use. If required or desired, it is activated by prereduction in a known manner and, if appropriate, also surface-passivated again before it is installed into the reactor for the aminating hydrogenation.
• the catalyst is, however, usually not reduced until within the reactor for the aminating hydrogenation. This is done in a manner known to the person skilled in the art by initial inertization with nitrogen or another inert gas.
• the reduction is performed with a hydrogenous gas as a pure gas phase or with inert circulation.
• the temperature at which this prereduction is performed is generally 5-200° C., preferably 20-150° C.
• the above-described catalysts are used in accordance with the invention in a process for preparing an amine by reacting an aldehyde and/or ketone with hydrogen and a nitrogen compound selected from the group of primary and secondary amines (aminating hydrogenation).
• the carbonyl compound is aminated preferably in the liquid phase.
• the catalyst is arranged in the reactor for the aminating hydrogenation (e.g. tubular reactor) preferably as a fixed bed.
• the reaction is performed in the liquid phase or in a mixed liquid/gas phase with at least 50% by weight of the reaction mixture in the liquid phase.
• the amination can be performed in trickle mode or in liquid-phase mode.
• the hydrogenation hydrogen added may be present in dissolved form in the liquid phase.
• the entrance temperature of the reactant mixture in the amination is, in one embodiment of the invention, from ⁇ 10 to 250° C., preferably from 0 to 180° C., in particular from 50 to 150° C.
• the nitrogen compound is used preferably in from 0.90 to 100 times the molar amount, especially in from 1.0 to 10 times the molar amount, based in each case on the aldehyde and/or ketone used.
• the process according to the invention is preferably performed at a catalyst hourly space velocity—measured as the mass of aldehyde or ketone in the feed based on the catalyst volume and the time—in the range from 0.01 to 2.00 kg (carbonyl compound)/liter (catalyst)/h, preferably from 0.10 to 1.50 kg/liter/h, more preferably from 0.20 to 1.20 kg/liter/h, especially preferably from 0.22 to 1.00 kg/liter/h.
• the process according to the invention is performed preferably at an absolute pressure in the range from 1 to 325 bar, preferably from 10 to 250 bar, more preferably from 100 to 200 bar, especially preferably from 85 to 150 bar, for example from 90 to 135 bar.
• the process according to the invention for aldehyde and/or ketone amination is performed preferably at a temperature in the range from 50 to 280° C., preferably from 80 to 250° C., more preferably from 120 to 210° C.
• the pressure in the reactor which arises from the sum of the partial pressures of the aminating agent, of the aldehyde and/or ketone component and of the reaction products formed at the temperatures specified, is appropriately increased by injecting hydrogen to the desired reaction pressure.
• the water of reaction formed in the course of the reaction generally does not have a disruptive effect on the conversion, the reaction rate, the selectivity and the catalyst lifetime and is therefore appropriately not removed therefrom until the workup of the reaction product, for example by distillation.
• Unconverted reactants and any suitable by-products which occur can be recycled back into the synthesis. Unconverted reactants can be flowed over the catalyst bed again in the cycle gas stream in discontinuous or continuous mode after the products have been condensed in the separator.
• R 1 , R 2 are each hydrogen (H), alkyl such as C 1-20 -alkyl, cycloalkyl such as C 3-12 -cycloalkyl, alkoxyalkyl such as C 2-30 -alkoxyalkyl, dialkylaminoalkyl such as C 3-30 -dialkylaminoalkyl, aryl, aralkyl such as C 7-20 -aralkyl and alkylaryl such as C 7-20 -alkylaryl, or together are —(CH 2 ) j —X—(CH 2 ) k —,
• R 3 , R 4 are each hydrogen (H), alkyl such as C 1-2 -alkyl, cycloalkyl such as C 3-12 -cycloalkyl, hydroxyalkyl such as C 1-20 -hydroxyalkyl, aminoalkyl such as C 1-20 -aminoalkyl, hydroxyalkylaminoalkyl such as C 2-20 -hydroxyalkylaminoalkyl, alkoxyalkyl such as C 2-30 -alkoxyalkyl, dialkylaminoalkyl such as C 3-30 -dialkylaminoalkyl, alkylaminoalkyl such as C 2-30 -alkylaminoalkyl, R 5 —(OCR 6 R 7 CR 8 R 9 ) n —(OCR 6 R 7 ), aryl, heteroaryl, aralkyl such as C 7-20 -aralkyl, heteroarylalkyl such as C 4-20 -heteroarylalkyl, alkyla
• R 2 and R 4 together are —(CH 2 ) l —X—(CH 2 ) m —,
• R 5 , R 10 are each hydrogen (H), alkyl such as C 1-4 -alkyl, alkylphenyl such as C 7-40 -alkylphenyl,
• R 6 , R 7 , R 8 , R 9 are each hydrogen (H), methyl or ethyl
• x is CH 2 , CHR 5 , oxygen (O), sulfur (S) or NR 5 ,
• Y is N(R 10 ) 2 , hydroxyl, C 2-20 -alkylaminoalkyl or C 3-20 -dialkylaminoalkyl,
• n is an integer from 1 to 30 and
• j, k, l, m, q are each integers from 1 to 4.
• the process according to the invention therefore preferably finds use for preparing an amine I by reacting an aldehyde and/or a ketone of the formula VI or VII
• R 1 , R 2 , R 3 and R 4 are each as defined above.
• reaction can also be effected intramolecularly in an appropriate amino ketone or amino aldehyde.
• Suitable ketones usable in accordance with the invention are, under the abovementioned prerequisites, virtually all aliphatic and aromatic ketones.
• the aliphatic ketones may be straight-chain, branched or cyclic; the ketones may comprise heteroatoms.
• the ketones may further bear substituents or comprise functional groups which behave inertly under the conditions of the hydrogenating amination, for example alkoxy, alkenyloxy, alkylamino or dialkylamino groups, or else, if appropriate, are hydrogenated under the conditions of the hydrogenating amination, for example C—C double or triple bonds,
• substituents or comprise functional groups which behave inertly under the conditions of the hydrogenating amination, for example alkoxy, alkenyloxy, alkylamino or dialkylamino groups, or else, if appropriate, are hydrogenated under the conditions of the hydrogenating amination, for example C—C double or triple bonds
• polyfunctional ketones are to be aminated, it is possible via the control of the reaction conditions to obtain amino ketones, amino alcohols, cyclic amines or polyaminated products.
• ketones Preference is given, for example, to aminatingly hydrogenating the following ketones: acetone, ethyl methyl ketone, methyl vinyl ketone, isobutyl methyl ketone, butanone, 3-methylbutan-2-one, diethyl ketone, tetralone, acetophenone, propiophenone, p-methylacetophenone, p-methoxyacetophenone, m-methoxyacetophenone, 1-acetylnaphthalene, 2-acetylnaphthalene, 1-phenyl-3-butanone, cyclobutanone, cyclopentanone, cyclopentenone, cyclohexanone, cyclohexenone, 2,6-dimethylcyclohexanone, cycloheptanone, cyclododecanone, acetylacetone, methylglyoxal and benzophenone.
• Suitable aldehydes usable in accordance with the invention are, under the abovementioned prerequisites, virtually all aliphatic and aromatic aldehydes.
• the aliphatic aldehydes may be straight-chain, branched or cyclic; the aldehydes may comprise heteroatoms.
• the aldehydes may further bear substituents or comprise functional groups which behave inertly under the conditions of the hydrogenating amination, for example alkoxy, alkenyloxy, alkylamino or dialkylamino groups, or else, if appropriate, are hydrogenated under the conditions of the hydrogenating amination, for example C—C double or triple bonds.
• polyfunctional aldehydes or keto aldehydes are to be aminated, it is possible via the control of the reaction conditions to obtain amino alcohols, cyclic amines or polyaminated products.
• aminating agents used in the hydrogenating amination of aldehydes and/or ketones in the presence of hydrogen may be primary or secondary, aliphatic or cycloaliphatic or aromatic amines.
• cyclic amines for example pyrrolidines, piperidines, hexamethyleneimines, piperazines and morpholines.
• the following mono- and dialkylamines are used as aminating agents: methylamine, dimethylamine, ethylamine, diethylamine, n-propylamine, di-n-propylamine, isopropylamine, diisopropylamine, dimethylmorpholine, isopropylethylamine, n-butylamine, di-n-butylamine, s-butylamine, di-s-butylamine, isobutylamine, n-pentylamine, s-pentylamine, isopentylamine, n-hexylamine, s-hexylamine, isohexylamine, cyclohexylamine, aniline, toluidine, piperidine, morpholine and pyrrolidine.
• Amines prepared with particular preference by the process according to the invention are, for example, N,N-di(C 1-4 -alkyl)cyclohexylamine (from cyclohexanone and di(C 1-4 -alkyl)amine), n-propylamines (such as dimethylpropylamine) (from propionaldehyde and DMA), N,N-dimethyl-N-isopropylamine (from acetone and DMA), N,N-dimethyl-N-butylamines (from butanal, i-butanal or butanone and DMA), N-ethyl-N,N-diisopropylamine (from acetaldehyde and N,N-diisopropylamine), cis-4-[3-(4-tert-butylphenyl)-2-methylpropyl]-2,6-dimethyl morpholine (from lysmeral and cis-2,6-dimethylmorph
• Al 2 O 3 extrudates (diameter 2.8 mm) having a surface area of 60-90 m 2 /g were treated with an impregnation solution comprising palladium nitrate, palladium nitrite and silver nitrate which has been acidified to a pH in the range from 0.2 to 2 with concentrated (69%) nitric acid.
• the content of the added nitric acid in the finished impregnation solution was 1.8% by weight.
• the moist extrudates were dried at 200° C. and calcined at 600° C.
• a catalyst was obtained which comprised 0.3% by weight of palladium and 0.1% by weight of silver, the weight ratio of palladium to silver being 3.
• the distribution of the elements over the extrudate cross section measured by the Electron Probe Microanalysis (EPMA) technique, was as follows:
• the following experiments were effected in an electrically heated 1 liter tubular reactor in a continuous reaction.
• the reaction effluents were analyzed by means of gas chromatography.
• the analysis programs used were: a) DB1 column, length 60 m; internal diameter 0.32 mm; helium carrier gas; temperature program: 80° C. then at 8° C./minutes to 280° C., finally 15 minutes isothermal at 280° C., and b) Rtx-5-amine column, length 30 m; internal diameter 0.32 mm; helium carrier gas; temperature program: 70° C. for 5 minutes, then at 5° C./minutes to 280° C., finally 10 minutes isothermal at 280° C.
• the product composition is reported as GC area percent of the crude effluents, calculated without water and without the excess of feedstock amine component.
• Fenpropimorph (cis-FPM) was prepared by reductive amination from technical-grade lysmeral (lyal) and cis-2,6-dimethylmorpholine (DMM) in the presence of hydrogen and of an inventive fixed bed catalyst. The reaction was performed in the liquid phase (liquid-phase or trickle mode).
• the technical-grade lysmeral (approx. 95% pure) and dimethylmorpholine (>97% pure) reactants were metered into the reactor with separate feeds at total pressure of from 50 to 140 bar, and reacted at from 200 to 240° C. in straight pass with liquid recycling.
• the synthesis was effected with a catalyst hourly space velocity of from 0.25 up to 0.50 kg (lyal)/(liter(cat.) ⁇ h) at a molar DMM/lyal ratio of 2.5.
• the lysmeral and dimethylmorpholine feedstocks were converted virtually quantitatively. The reaction proceeded very selectively, which is why only small amounts of secondary components were present in the reaction effluent.
• Fenpropimorph was prepared by reductive amination from technical-grade lysmeral and cis-2,6-dimethylmorpholine in the same reactor as in Example 1.
• the catalyst used was a silver- and palladium-containing fixed bed catalyst which had silicon dioxide as a support and did not have a coating structure of the catalytically active metals.
• the experiments were otherwise performed under comparable reaction conditions. Owing to a comparatively low catalyst activity, increased enamine contents in the reaction effluent were often determined. The reaction proceeded less selectively; lysmerol was formed as a secondary component to an increased extent.
• the experimental results are compiled in the following Table 2.
• N,N-Dimethylcyclohexylamine (DMCHA) is prepared by reductive amination from cyclohexanone (anon) and dimethylamine (DMA) in the presence of hydrogen and of an inventive fixed bed catalyst. The reaction is performed in the liquid phase in trickle or liquid-phase mode.
• the cyclohexanone (99.5% pure) and dimethylamine (>99% pure) reactants were metered into the reactor at total pressure from 90 to 130 bar.
• the separate feeds were mixed upstream of the reactor.
• the reaction was effected at from 160 to 220° C. in straight pass without liquid recycling.
• the synthesis was effected with a catalyst hourly space velocity of from 0.15 up to 0.80 kg (anon)/(liter(cat.) ⁇ h) at a molar DMA/anon ratio of from 2.3 to 3.0.
• the cyclohexanone and dimethylamine feedstocks were converted virtually quantitatively.
• the reaction proceeded very selectively, which is why only small amounts of alcohol (cyclohexanol) were present in the reaction effluent.
• Another side reaction was “scrambling”, the formation of monomethylcyclohexylamine (MMCHA) by methyl group migration in DMCHA and DMA.
• Table 3 The experimental results are listed in the following Table 3.
• N,N-Dimethylcyclohexylamine was prepared by reductive amination of cyclohexanone and dimethylamine in the same reactor as in Example 2.
• the catalyst used was a silver- and palladium-containing fixed bed catalyst which had silicon dioxide as a support and did not have a coating structure of the catalytically active metals.
• the experiments were otherwise performed under comparable reaction conditions. The reaction proceeded less selectively; cyclohexanol was formed as a secondary component by hydrogenation of cyclohexanone to an increased extent.
• the experimental results are compiled in Table 4.

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